Synthetic borneol processing system and processing method

Abstract

The application provides a synthetic borneol processing system. The synthetic borneol processing system comprises a side wall arranged in a receiving space, a saponification reaction section, a borneol solution production section, a borneol crystallization section and a tail gas production section arranged in sequence and received in the receiving space. The saponification reaction section comprises a feed inlet penetrating through the side wall, a plurality of reaction trays arranged in parallel and spaced apart in the saponification reaction section, and a plurality of steam inlets penetrating through the side wall and corresponding to the reaction tray group. The reaction tray group defines the saponification reaction section to form gas phase channels and liquid phase channels with different flow directions. The synthetic borneol processing system of the application realizes continuous saponification reaction and continuous separation and extraction of synthetic borneol, and the saponification reaction and the separation and extraction process are carried out synchronously, thereby reducing the generation of by-products and increasing the recovery rate of synthetic borneol. Meanwhile, the application also provides a synthetic borneol processing method using the above processing system.

Description

[Technical Field]

[0002] This invention relates to the field of synthetic borneol processing technology, and more particularly to a continuous saponification reaction and purification separation processing method and system for synthetic borneol. [Background Technology]

[0004] Borneol (1,7,7-trimethylbicyclo[2,2,1]hepta-2-ol), also known as camphor, is divided into natural camphor and synthetic camphor. Synthetic camphor is obtained by distillation after esterification and saponification reactions, followed by dissolution of the crude camphor with a solvent and further crystallization to form a flaky structure.

[0005] In existing synthetic borneol production processes, crude borneol is often obtained by saponification of borneol oxalate with alkaline solution, followed by steam distillation and cooling crystallization in a condenser.

[0006] In the existing synthetic borneol saponification reaction, the processing of synthetic borneol involves feeding the esterified raw material into a saponification distillation pot as a saponification reaction liquid. The saponification distillation pot is maintained at 100°C to ensure the entire saponification reaction proceeds. This requires introducing the vapor containing the synthetic borneol into a crystallization and condensation device for treatment. Furthermore, the crude borneol produced after the saponification reaction is mixed with the vapor and cannot be effectively separated. It is necessary to use relevant equipment to cool the mixed gas and allow the synthetic borneol to solidify, which facilitates the collection of borneol.

[0007] However, the saponification reaction device and condensation separation device for borneol mentioned above are independent of each other, and their structures and processes are complex, resulting in slow separation speed, poor efficiency, and high cost. Therefore, it is necessary to provide a new, efficient processing system and method for separating and extracting borneol to effectively solve the above-mentioned technical problems. [Summary of the Invention]

[0009] In view of the technical problems of existing borneol saponification reaction and separation extraction being independent, unable to operate continuously, and having complex extraction processes, low efficiency, and low purity, the purpose of this invention is to provide a synthetic borneol processing system that achieves continuous and efficient saponification reaction and continuous separation extraction, thereby improving efficiency, simplifying the process, increasing purity, and reducing costs.

[0010] The present invention also provides a processing method for extracting ice flakes using the above-mentioned synthetic ice flake processing system.

[0011] To achieve the above objectives, the present invention provides a synthetic borneol processing system, comprising a sidewall forming a containment space, and sequentially connected and contained within the containment space a saponification reaction section, a borneol solution production section, a borneol crystallization section, and a tail gas production section. The saponification reaction section includes a feed inlet penetrating the sidewall, a plurality of parallel reaction trays spaced apart in the saponification reaction section, and a plurality of steam inlets. The steam inlets penetrate the sidewall and correspond to the reaction trays. The reaction trays define the saponification reaction section, forming a gas phase channel and a liquid phase channel with opposite flow directions.

[0012] A method for processing borneol includes the following steps:

[0013] The reaction liquid is fed into the saponification reaction section through the feed inlet. The saponification reaction section includes a feed inlet, multiple reaction trays, and a steam inlet.

[0014] The reaction tower tray assembly includes a liquid phase channel and a gas phase channel. The reaction liquid flows from top to bottom in the liquid phase channel, while the vapor and gaseous ice flakes flow from bottom to top in the gas phase channel, with the two flowing in opposite directions.

[0015] Steam is continuously supplied into the saponification reaction section from the steam inlet;

[0016] A borneol recovery section is provided to receive liquid products and unreacted reactants from the saponification reaction section for secondary saponification and discharge byproducts.

[0017] A borneol crystallization section is provided, which receives gaseous borneol from the saponification reaction section, and after crystallization and solvent absorption, a borneol solution is produced.

[0018] Compared with related technologies, the processing system of the present invention integrates the saponification reaction and crystallization process into one system, replacing the independent functional modules of the prior art. It can be used simply, quickly and efficiently to separate borneol from reaction solutions containing borneol, and is also conducive to further purification to obtain borneol with high purity and high yield. [Attached Image Description]

[0020] To more clearly illustrate the technical solutions in the embodiments of the present invention, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort, wherein:

[0021] Figure 1 This is a three-dimensional structural diagram of the continuous saponification reaction and separation extraction processing system for synthesizing borneol disclosed in the first embodiment of the present invention;

[0022] Figure 2 for Figure 1 An exploded three-dimensional schematic diagram of the machining system shown.

[0023] Figure 3 for Figure 1 A side sectional view of the synthetic ice flake processing system shown.

[0024] Figure 4 yes Figure 3 A magnified view of a portion of region VI of the saponification reaction section shown;

[0025] Figure 5 This is a schematic flowchart of a method for processing borneol provided by the present invention;

[0026] Figure 6 This is a three-dimensional schematic diagram of the reaction tray assembly of the synthetic borneol processing system disclosed in the second embodiment of the present invention;

[0027] Figure 7 yes Figure 6 The top view of the reaction tower tray assembly shown.

Detailed Implementation Methods

[0029] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of them. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0030] Please see Figure 1 This is a three-dimensional structural diagram of a synthetic borneol processing system 100, as disclosed in the first embodiment of the present invention, for continuous saponification reaction and borneol extraction. The borneol processing system 100 is a processing device for realizing continuous borneol saponification reaction and continuous extraction and separation of synthetic borneol, and its overall structure is tower-shaped. The borneol processing system 100 includes a sidewall 10, a borneol recovery section 11, a saponification reaction section 13, a borneol solution production section 15, a borneol crystallization section 17, and a tail gas production section 19. The sidewall 10 is arranged to form a receiving space open at both ends. Along the extending direction of the sidewall 10, different functional areas are defined as the borneol recovery section 11, the saponification reaction section 13, the borneol solution production section 15, the borneol crystallization section 17, and the tail gas production section 19. The borneol recovery section 11 and the tail gas production section 19 are respectively located at two opposite ends of the tower-shaped structure. From the borneol recovery section 11 to the tail gas output section 19, the saponification reaction section 13, the borneol solution output section 15, and the borneol crystallization section 17 are sequentially connected.

[0031] Please refer to the following: Figure 2 , Figure 3 and Figure 4,in Figure 2 for Figure 1 The diagram shown is a three-dimensional exploded view of the synthetic borneol processing system. Figure 3 yes Figure 1 The side sectional view of the synthetic borneol processing system shown is shown. Figure 4 yes Figure 3 The diagram shows a partially enlarged view of region IV. The saponification reaction section 13 is a functional module that realizes the saponification reaction between the borneol esterification liquid and the alkali. The saponification reaction section 13 includes a feed inlet 131, multiple reaction tray groups 133, and multiple steam inlets 135. The feed inlet 131 is located on the side wall 10 where the saponification reaction section 13 is located and penetrates the side wall 10. In this embodiment, there are three reaction tray groups 133, which are arranged in parallel and spaced apart along the direction from the borneol recovery section 11 to the tail gas production section 19. There are also three steam inlets 135, which penetrate the side wall 10 where the saponification reaction section 13 is located, and each reaction tray group 133 corresponds to one of the steam inlets 135. The feed inlet 131 is higher than the steam inlets 135.

[0032] The feed inlet 131 serves as the input end of the borneol processing system 100, providing borneol esterification liquid and strong alkali into the borneol processing system 100 as raw materials before the saponification reaction. Along the direction from the borneol recovery section 11 to the tail gas output section 19, the height of the feed inlet 131 is higher than that of the reaction tray assembly 133.

[0033] Please refer to the following: Figure 2 and Figure 4 The reaction tray assembly 133 includes a horizontal tray 1331, an inclined tray 1333, a downcomer 1335, and a receiving tray 1337.

[0034] The horizontal tray 1331 is generally in the shape of a disc plate, perpendicular to the side wall 10 and sandwiched within the receiving space. The edge of the horizontal tray 1331 is in contact with the inner surface of the side wall 10. The horizontal tray 1331 is provided with a plurality of first guide holes 1332 and first sieve holes 1334. The extending direction of the first guide holes 1332 is parallel to the extending direction of the side wall 10, and the extending direction of the first sieve holes 1334 is parallel to the direction of the horizontal tray 1331.

[0035] The tilted tray 1333 is generally elliptical in shape and is tilted within the receiving space of the side wall 10, forming a relatively high end 13331 and a low end 13333. The high end 13331 is located near the exhaust gas production section 19, and the low end 13333 is located near the ice flake recovery section 11. The tilted tray 1333 and the horizontal tray 1331 are set at an angle to each other, with the angle value between 10 degrees and 15 degrees. The tilted tray 1333 is provided with a plurality of second guide holes 1336 and second sieve holes 1338. The extension direction of the second guide holes 1336 is perpendicular to the extension direction of the tilted tray 1333, and the extension direction of the second sieve holes 1338 is parallel to the direction of the tilted tray 1333.

[0036] The downcomer 1335 is a hollow tube that penetrates the edge region of the horizontal tray 1331 and also penetrates the lower end 13333 of the tilted tray 1333. Extending along the sidewall 10, one end of the downcomer 1335 extends to the upper side of the tilted tray 1333, and the other end extends to the lower side of the horizontal tray 1331. One end of the downcomer 1335 is higher than the upper surface of the tilted tray 1333, while the height of the downcomer 1335 is lower than the upper end 13331 of the tilted tray 1333. This creates an inverted conical reaction tank space between the upper surface of the tilted tray 1333 and the outer surface of the downcomer 1335, within which the borneol esterification solution and the strong alkali undergo a saponification reaction.

[0037] The downcomer 1335 is provided with a baffle 13353. The baffle 13353 forms a gas phase channel 13355 and a liquid phase channel 13357 by separating the downcomer 1335. At the end of the downcomer 1335 that is lower than the horizontal tray 1331, the inlet of the gas phase channel 13355 and the outlet of the liquid phase channel 13357 are flush with each other; at the end of the downcomer 1335 that is higher than the horizontal tray 1331, the outlet of the gas phase channel 13355 is higher than the inlet of the liquid phase channel 13357.

[0038] The receiving tray 1337 is located at the edge of the inclined tray 1333 and is opposite to the downcomer 1335. In two adjacent reaction tray groups 133, the downcomer 1335 of one reaction tray group 133 and the receiving tray 1337 of the other reaction tray group 133 are located on the same side of the sidewall 10. Specifically, in this embodiment, the receiving tray 1337 of the highest reaction tray group 133, the downcomer 1335 of the second highest reaction tray group 133, and the receiving tray 1337 of the third highest reaction tray group 133 are located on one side of the sidewall 10. Figure 3As shown on the right side; the downcomer 1335 of the reaction tray assembly 133 at the highest position, the liquid receiving tray 1337 of the reaction tray assembly 133 at the second highest position, and the downcomer 1335 of the reaction tray assembly 133 at the third highest position are located on the other side of the side wall 10. Figure 3 The left side is shown.

[0039] When the reaction tower tray assembly 133 is in operation, it includes the following steps:

[0040] First, a saponification reaction solution is provided into the saponification reaction section 13 through the feed inlet 131. The saponification reaction solution includes borneol esterification solution and strong alkali.

[0041] Secondly, the saponification reaction liquid flows along the high end 13331 of the inclined tray 1333 to the low end 13333 of the inclined tray 1333. Part of the saponification reaction liquid accumulates in the reaction tank space, and part of the saponification reaction liquid leaks into the horizontal tray 1331 through the second guide hole 1336. On the other hand, steam is continuously supplied from the steam inlet 135 into the saponification reaction section 13, and the steam enters the reaction tank space through the second guide hole 1336.

[0042] Furthermore, as the saponification reaction liquid further enters the saponification reaction section 13 from the feed inlet 131, when the liquid level of the saponification reaction liquid is higher than the liquid phase channel 13357, the excess saponification reaction liquid flows down from the liquid phase channel 13357 of the downcomer 1335 to another reaction tray group 133.

[0043] In this process, the feed inlet 131 is positioned higher than the steam inlet 135 and also higher than the high end 13331, and is located on the same side of the side wall 1 as the high end 13331. The steam inlet 135 penetrates the side wall 10 between the high end 13331 of the horizontal tray 1331 and the high end 13331 of the inclined tray 1333, continuously supplying the saponification reaction liquid into the saponification reaction section 13 through the feed inlet 131. Simultaneously, steam is continuously supplied from the steam inlet 135 into the saponification reaction section 13, stirring the saponification reaction liquid, accelerating the flow rate of the saponification reaction liquid, promoting the saponification reaction, sublimating the camphor produced by saponification, and minimizing or preventing the leakage of the saponification reaction liquid through the second guide hole 1336 to another reaction tray group 133, so that the entire saponification reaction is continuous, sufficient, and efficient within the saponification reaction tank space to obtain camphor.

[0044] Please refer to it again. Figure 3Along the direction from the borneol recovery section 11 to the tail gas production section 19, the three reaction tray groups 133 are arranged in parallel and spaced apart. Correspondingly, the liquid byproducts generated from the reaction tray group 133 at the highest position and the unreacted saponification reaction liquid enter the reaction tray group 133 at the lower position through the liquid phase channel 13357 of the downcomer 1335 for secondary reaction.

[0045] Furthermore, the liquid byproducts and unreacted saponification reaction liquid after the reaction in the second-highest reaction tray group 133 enter the lowest-position reaction tray group 133 again through the liquid phase channel 13357 of the downcomer 1335 for another saponification reaction.

[0046] And so on.

[0047] Three reaction tray groups 133 are sequentially arranged along the direction from the tail gas output section 19 to the borneol recovery section 11, forming three consecutive saponification reactions to ensure the full occurrence of the saponification reaction. For those skilled in the art, the number of reaction tray groups 133 can be adjusted according to actual processing needs, for example, it can be set to four or other numbers to ensure a complete saponification reaction. That is, depending on the number of reaction tray groups 133 arranged sequentially, the liquid byproducts and incompletely reacted saponification reaction liquid from the higher reaction tray group 133 will flow sequentially to the lower reaction tray group 133 for a second saponification reaction along the direction from the tail gas output section 19 to the borneol recovery section 11.

[0048] In the above saponification reaction process, the steam temperature is set to superheated steam at 110 degrees Celsius. As is well known, the sublimation temperature of borneol is between 90 and 110 degrees Celsius. The steam is blown into the reaction tank space through the second guide hole 1336 of the inclined tray 1333, causing the sublimated gaseous borneol to flow from the borneol recovery section 11 to the tail gas production section 19. Between adjacent reaction tray groups 133, the gaseous borneol and steam flow along the gas phase channel 13355 of the downcomer 1335, that is, in the opposite direction to the liquid byproducts and the insufficiently reacted saponification reaction liquid.

[0049] At this point, after passing through the saponification reaction section 13, byproducts and sublimated borneol are generated, wherein the byproducts are in liquid form and flow toward the borneol recovery section 11, and the sublimated gaseous borneol flows toward the borneol solution production section 15.

[0050] The borneol recovery section 11 includes a recovery section steam inlet 111, a reactant outlet 113, and a secondary reaction tank 115. The recovery section steam inlet 111 penetrates the side wall 10 and communicates with the secondary reaction tank 115. The reactant outlet 113 is located at the bottom of the tower-shaped structure and communicates with the secondary reaction tank.

[0051] When the camphor recovery section 11 is in operation, it includes the following steps:

[0052] First, the borneol recovery section 11 receives the byproducts and unreacted borneol esterification liquid and strong alkali from the saponification reaction section 13, and then performs a second saponification reaction in the secondary reaction tank 115.

[0053] Secondly, steam is supplied from the steam inlet 111 of the recovery section into the secondary reaction tank 115 for gas stirring, and the camphor generated after the secondary saponification reaction is sublimated and flows to the saponification reaction section 13.

[0054] Furthermore, the byproducts after the secondary reaction are detected. When the camphor content is less than 0.2%, the corresponding byproducts are discharged through the reactant outlet 113.

[0055] During the operation of the borneol recovery section 11, given that byproducts, unreacted borneol esterification liquid, and strong alkali are continuously supplied from the saponification reaction section 13 to the secondary reaction tank 115, steam is continuously supplied to sublimate the synthetic borneol generated after the secondary reaction through gas stirring. The sublime borneol then flows to the saponification reaction section 13, and byproducts with a borneol content of less than 0.2% are discharged from the reactant outlet 113. This improves the borneol recovery rate, reduces the borneol content in the excrement, and is beneficial to environmental protection.

[0056] Please refer to it again. Figure 2 and Figure 3 The borneol solution production section 15 includes a support plate 151, multiple gas pipes 153, a borneol solution outlet 155, and a heating jacket 157. The multiple gas pipes 153 penetrate the support plate 151 and connect the saponification reaction section 13 and the borneol crystallization section 17. The gas pipes 153 are evenly arrayed on the support plate 151. The borneol solution outlet 155 penetrates the side wall 10 and is positioned above the support plate 151. The heating jacket 157 provides a heating environment to prevent borneol crystallization from clogging the gas pipes 153.

[0057] When gaseous borneol from the saponification reaction section 13 enters the borneol solution production section 15 via the gas pipe 153, it then flows to the borneol crystallization section 17.

[0058] The sidewall 10, together with the outer walls of the support plate 151 and the air pipe 153, forms a receiving space to receive the liquid camphor solution generated from the camphor crystallization section 17, and then outputs it to the camphor crystallization device through the camphor solution outlet 155. In this camphor solution production section, the liquid camphor solution is a liquid solution composed of liquid camphor and an organic solvent.

[0059] Please refer to it again. Figure 2 and 3 The borneol crystallization section 17 includes a cooling jacket 171, a crystallization filler 173, and an absorbent spraying module 175.

[0060] The cooling jacket 171 is fitted around the side wall 10 to provide a cooling environment, allowing the ice flakes to crystallize fully. In this embodiment, the cooling jacket 171 is filled with -7 degrees Celsius frozen brine as a refrigerant to control the working environment of the ice flake crystallization section 17 at a set temperature, such as zero degrees Celsius, thereby ensuring that the gaseous ice flakes generated from the saponification reaction section 13 crystallize into the crystallization filler 173 after passing through the gas pipe 153.

[0061] The crystallizing filler 173 is a honeycomb carrier. When gaseous ice flakes enter the crystallizing filler 173 through the gas tube 153, the gaseous ice flakes crystallize based on the set ice flake crystallization environment. In this invention, the crystallizing filler 173 can be a filler, specifically a metal filler.

[0062] The absorbent spraying module 175 is located near the exhaust gas output section 19. It sprays organic solvents, such as NMP, THF and gasoline, into the crystal filler 173 to effectively dissolve camphor crystals and obtain a liquid camphor-containing solution, i.e., camphor solution. The liquid camphor solution flows to the receiving space enclosed by the support plate 151 and the side wall 10, and then leaks out from the camphor solution outlet 155.

[0063] The exhaust gas output section 19 includes a top wall 191, an anti-fog net 193, and an exhaust gas outlet 195. The top wall 191 covers the top of the tower-shaped structure, and the anti-fog net 193 is located adjacent to the absorbent spraying module 175. The exhaust gas outlet 195 penetrates the top wall 191 and connects to the external environment to the camphor processing system 100. The exhaust gas generated during camphor processing is discharged to the external environment through the exhaust gas outlet 195.

[0064] Please see Figure 5 The present invention also provides an ice-processing method for the ice-processing system 100, which includes the following steps:

[0065] S01. Provide the reaction liquid into the saponification reaction section from the feed inlet. The saponification reaction section includes a feed inlet, multiple reaction tray groups and a steam inlet.

[0066] S02. The reaction tower tray assembly includes a liquid phase channel and a gas phase channel. The reaction liquid flows from top to bottom in the liquid phase channel, while the vapor and gaseous ice flakes flow from bottom to top in the gas phase channel, with the two flowing in opposite directions.

[0067] S03. Provide steam continuously into the saponification reaction section from the steam inlet;

[0068] S04. Provide a borneol recovery section to receive liquid products and unreacted reactants from the saponification reaction section for secondary saponification reaction and discharge by-products;

[0069] S05. Provide a borneol crystallization section to receive gaseous borneol from the saponification reaction section, and produce a borneol solution after crystallization and solvent absorption;

[0070] S06. Provide a tail gas output section to receive and discharge the tail gas from the saponification reaction section after camphor crystallization.

[0071] In the borneol processing system 100 of the present invention, the tower-shaped structure is arranged from bottom to top as follows: borneol recovery section 11, saponification reaction section 13, borneol solution output section 15, borneol crystallization section 17, and tail gas output section 19. Each reaction section sequentially realizes the continuous process of saponification reaction, borneol separation and extraction, and secondary saponification reaction, achieving continuous operation. Compared with the prior art, the borneol processing system of the present invention performs borneol separation and extraction simultaneously with the saponification reaction, continuously outputs borneol solution, reduces the generation of by-reactants, reduces the borneol content in borneol by-reactants, increases production capacity, and reduces pollution.

[0072] More importantly, in the saponification reaction section 13 of this invention, multiple reaction tray groups 133 are added, arranged freely and parallelly at intervals along the height direction as needed, so that the insufficiently reacted borneol esterification liquid and strong alkali can react fully from top to bottom. On the other hand, the reaction tray group 133 is assembled by using the horizontal tray 1331 in conjunction with the inclined tray 1333 and the downcomer 1335, forming a bidirectional flow structure with separation of gas and liquid phases, achieving continuous processing. Furthermore, the inclined tray 1333 is tilted, increasing the contact area between the hot steam and the saponification liquid, which is beneficial for borneol extraction.

[0073] Furthermore, in the saponification reaction section 13 of the present invention, a plurality of first guide holes 1332 are provided on the horizontal tray 1331, and a plurality of second guide holes 1336 are provided on the inclined tray 1333. The steam passes through the first guide holes 1332 and the second guide holes 1336, which can accelerate the flow rate of the saponification reaction liquid on the one hand, and control the temperature of the horizontal tray 1331 and the inclined tray 1333 to be constant on the other hand, preventing ice flakes from crystallizing on the trays and causing blockage.

[0074] Please see Figure 6 and Figure 7 ,in, Figure 6 This is a three-dimensional schematic diagram of the reaction tray assembly of the synthetic borneol processing system disclosed in the second embodiment of the present invention. Figure 7 yes Figure 6 The diagram shows a top view of the reaction tray assembly. This embodiment is basically the same as the first embodiment, except that the downcomer 2335 may not have a baffle, forming a liquid phase channel 23357. The reaction tray assembly 233 also includes a gas phase pipe 239, which forms a gas phase channel 2395. The gas phase pipe 239 is arranged through the inclined tray 2333 and the horizontal tray 2331. The downcomer 2335, the gas phase pipe 239, and the receiving tray 237 are arranged around the edge of the inclined tray 2333. The height of the gas phase pipe 239 relative to the inclined tray 2333 is at least twice the height of the overflow weir 2371 of the receiving tray 237.

[0075] There are two gas phase pipes 239. Along the edge of the inclined tray 2333, the downcomer 2335, one gas phase pipe 239, the receiving tray 237, and the other gas phase pipe 239 are arranged in sequence. The downcomer 2335 is arranged opposite to the receiving tray 237, and the two gas phase pipes 239 are arranged opposite to each other.

[0076] It is understood that the number of gas phase tubes 239 can be set by those skilled in the art as needed, and is not limited to two, but can be one, three, four, etc., and is not specifically limited here.

[0077] The above description is merely an embodiment of the present invention. It should be noted that those skilled in the art can make improvements without departing from the inventive concept of the present invention, but these improvements all fall within the protection scope of the present invention.

Claims

1. A synthetic camphor processing system, comprising: a side wall, which is annularly arranged to form a receiving space; a saponification reaction section, a camphor solution production section, a camphor crystallization section and a tail gas production section, which are sequentially connected and received in the receiving space, wherein the saponification reaction section comprises: a feed inlet, which penetrates the side wall; a plurality of reaction tray groups, which are arranged in parallel and spaced apart in the saponification reaction section; a plurality of steam inlets, which penetrate the side wall and correspond to the reaction tray groups, and the reaction tray groups define the saponification reaction section to form gas phase channels and liquid phase channels with different flow directions, the reaction tray groups comprise horizontal trays, inclined trays, downcomers and receiving trays, the horizontal trays are arranged perpendicularly to the side wall, the inclined trays are arranged at an angle to the horizontal trays, the downcomers penetrate the inclined trays and the horizontal trays, the receiving trays are arranged on the inclined trays and opposite to the downcomers, and in adjacent two reaction tray groups, the downcomer of one reaction tray group and the receiving tray of the other reaction tray group are arranged on the same side of the side wall.

2. The synthetic ice sheet processing system of claim 1, wherein, defining the high end of the inclined tray adjacent to the tail gas production section and the low end of the inclined tray adjacent to the saponification reaction section, the downcomer is arranged adjacent to the low end, the outer surface of the downcomer cooperates with the surface of the inclined tray to form a reaction pool space, and the steam inlet is arranged between the high end and the low end.

3. The synthetic ice sheet processing system of claim 2, wherein, the downcomer is provided with a partition plate, the partition plate separates the downcomer to form the gas phase channels and the liquid phase channels, and the port height of the gas phase channels adjacent to the tail gas production section is higher than the port height of the liquid phase channels adjacent to the tail gas production section.

4. The synthetic ice sheet manufacturing system of claim 2, wherein, the downcomer forms the liquid phase channels, the reaction tray group further comprises a gas phase pipe, the gas phase pipe forms the gas phase channels, the gas phase pipe penetrates the inclined tray and the horizontal tray, and the downcomer, the gas phase pipe and the receiving tray are arranged along the edge of the inclined tray, the height of the gas phase pipe relative to the inclined tray is higher than the height of the overflow weir of the receiving tray.

5. The synthetic ice sheet processing system of claim 4, wherein, the number of the gas phase pipes is two, and the downcomer, one gas phase pipe, the receiving tray and the other gas phase pipe are sequentially arranged along the edge direction of the inclined tray.

6. The synthetic ice sheet processing system of claim 2 or 4, wherein, the horizontal tray comprises a plurality of first guide holes and first screen holes, and the inclined tray comprises a plurality of second guide holes and second screen holes.

7. The synthetic ice sheet manufacturing system of claim 1, wherein, the camphor solution production section comprises a support plate and a gas pipe, the support plate is arranged perpendicularly to the side wall, the gas pipe penetrates the support plate and is arranged in an array on the support plate.

8. The synthetic ice sheet manufacturing system of claim 7, wherein, the camphor solution production section further comprises a heating jacket and a camphor solution outlet, the camphor solution outlet is arranged adjacent to the support plate, and the heating jacket is sleeved on the periphery of the side wall.

9. The synthetic ice sheet manufacturing system of claim 1, wherein, the processing system further comprises a camphor recovery section, which is arranged on the side of the saponification reaction section away from the camphor solution production section, the camphor recovery section comprises a steam inlet, a reactant outlet and a secondary reaction pool, the steam inlet penetrates the side wall and communicates with the secondary reaction pool, and the reactant outlet is arranged at the bottom of the processing system and communicates with the secondary reaction pool.

10. The synthetic ice sheet manufacturing system of claim 1, wherein, The tail gas outlet section comprises a top wall, a fog prevention net and a tail gas outlet, the top wall is arranged at the end of the processing system, the tail gas outlet penetrates through the top wall, and the fog prevention net is arranged close to the ice flake crystallization section.

11. A method for processing ice flakes applied to the synthetic ice flake processing system of claim 1, characterized by, The method comprises the following steps: The reaction liquid is fed into the saponification reaction section from a feeding port, the saponification reaction section comprises a feeding port, a plurality of reaction tray groups and a steam inlet; The reaction tray group comprises a liquid phase channel and a gas phase channel, the reaction liquid flows from top to bottom in the liquid phase channel, and steam and gaseous borne ice flakes flow from bottom to top along the gas phase channel, and the flowing directions of the two are different; Steam is continuously fed into the saponification reaction section from the steam inlet; An ice flake recovery section is provided, which receives the liquid phase product and the unreacted reaction substance from the saponification reaction section to perform secondary saponification reaction, and discharges by-products; An ice flake crystallization section is provided, which receives gaseous borne ice flakes from the saponification reaction section, and forms ice flake solution product after crystallization and solvent absorption.

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